WO2013014081A1 - Catalyst for the conversion of oxygenates to olefins and a process for preparing said catalyst - Google Patents
Catalyst for the conversion of oxygenates to olefins and a process for preparing said catalyst Download PDFInfo
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- WO2013014081A1 WO2013014081A1 PCT/EP2012/064300 EP2012064300W WO2013014081A1 WO 2013014081 A1 WO2013014081 A1 WO 2013014081A1 EP 2012064300 W EP2012064300 W EP 2012064300W WO 2013014081 A1 WO2013014081 A1 WO 2013014081A1
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- Prior art keywords
- catalyst
- suz
- zeolite
- conversion
- oxygenates
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Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 74
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 32
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 title description 4
- 239000010457 zeolite Substances 0.000 claims abstract description 42
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 34
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 150000001298 alcohols Chemical class 0.000 claims abstract description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical group OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 47
- 238000000034 method Methods 0.000 claims description 14
- 230000008569 process Effects 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000011260 aqueous acid Substances 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 2
- 150000002170 ethers Chemical class 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 13
- 230000015572 biosynthetic process Effects 0.000 description 11
- 238000003786 synthesis reaction Methods 0.000 description 9
- 239000013078 crystal Substances 0.000 description 7
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000002441 X-ray diffraction Methods 0.000 description 5
- 229930195733 hydrocarbon Natural products 0.000 description 5
- 150000002430 hydrocarbons Chemical class 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000002290 gas chromatography-mass spectrometry Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000010561 standard procedure Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 229940073455 tetraethylammonium hydroxide Drugs 0.000 description 4
- LRGJRHZIDJQFCL-UHFFFAOYSA-M tetraethylazanium;hydroxide Chemical compound [OH-].CC[N+](CC)(CC)CC LRGJRHZIDJQFCL-UHFFFAOYSA-M 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 238000003917 TEM image Methods 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 241000894007 species Species 0.000 description 3
- 238000010025 steaming Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000004809 Teflon Substances 0.000 description 2
- 229920006362 Teflon® Polymers 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 238000001000 micrograph Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000001878 scanning electron micrograph Methods 0.000 description 2
- 238000004626 scanning electron microscopy Methods 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 239000005995 Aluminium silicate Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 230000005526 G1 to G0 transition Effects 0.000 description 1
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 238000002003 electron diffraction Methods 0.000 description 1
- 238000011066 ex-situ storage Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000012229 microporous material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000010943 off-gassing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 235000013849 propane Nutrition 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000000550 scanning electron microscopy energy dispersive X-ray spectroscopy Methods 0.000 description 1
- 150000004760 silicates Chemical class 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004627 transmission electron microscopy Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/06—Washing
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
- C07C1/22—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms by reduction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/16—After treatment, characterised by the effect to be obtained to increase the Si/Al ratio; Dealumination
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/36—Steaming
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/37—Acid treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
Definitions
- the present invention relates to a catalyst, which is suit ⁇ able for use in the process where oxygenates, i.e. chemical compounds containing oxygen as part of their structure (e.g. alcohols or ethers) are converted to olefins.
- oxygenates i.e. chemical compounds containing oxygen as part of their structure (e.g. alcohols or ethers) are converted to olefins.
- a meth- od for the formation of the catalyst is also provided.
- the invention concerns a catalyst for the conversion of oxygenates to olefins, said catalyst being based on SUZ-4 zeolite.
- the SUZ-4 zeolite is modified in a number of ways with the purpose to yield a catalyst with improved properties for the conversion of oxygenates to olefins .
- the SUZ-4 zeolite has been given the three-letter IUPAC designation code SZR.
- the 10-membered ring channels of the SUZ-4 zeolite are the main straight channels in the framework, and they are interconnected by zig-zag 8-ring channels.
- the 10-ring straight channels of the SUZ-4 zeo- lite have dimensions of 4.6 x 5.2 A, i.e.
- EP 0 706 984 Al discloses the catalytic use of SUZ-4 zeolite for the isomerisation of hydrocarbons, and in US 6,514,470 B2 (University of California) a large number of aluminium-silicate materials, including SUZ-4 ze ⁇ olite, are used as catalysts for lean burn exhaust abate ⁇ ment.
- JP 2009-233620 A describes the use of SUZ-4 zeolite in an SCR catalyst with the objective to give the catalyst improved hydrothermal durability.
- the invention concerns a catalyst for the conversion of oxygenates to olefins, said catalyst consisting essentially of a selected SUZ-4 zeolite.
- the catalyst according to the invention is characterised in that the zeolite has a Si/Al ratio of at least 20, preferably between 20 and 500. The most preferred Si/Al ratio in the zeolite is between 20 and 100.
- step (b) increasing the Si/Al ratio to 20 or above by con- tacting the product of step (a) with water vapour at elevated temperatures.
- step (b) is preferably performed at a temperature of 400-700°C. Furthermore it is preferred to perform step (b) for 1-12 hours by feeding 1-20 g 3 ⁇ 40 per g of catalyst per hour.
- the SUZ-4 catalyst resulting from step (b) of the process is preferably washed with an aqueous acid solution.
- the catalyst according to the invention is used for the conversion of oxygenates to olefins.
- the oxygenates to be converted to olefins are preferably selected from the group consisting of CI to C4 alcohols.
- the most preferred oxygen- ate to be converted to an olefin is methanol.
- Fig. 5 shows GC-MS chromatograms of SAPO-34, SUZ-4, and ZSM-5 catalysts tested under identical reaction conditions after 5 minutes on stream.
- the SUZ-4 zeolite-based catalyst is synthesized in a manner known per se by preparing (i) a solution of Al-wire in aqueous MOH, where M is an alkali metal, (ii) a 25 wt% so ⁇ lution of tetraethylammonium hydroxide (TEAOH) and (iii) a 40 wt% solution of Ludox-AS 40, mixing the solutions (i)- (iii) at 60°C and crystallizing the resultant gel at 160°C with stirring, followed by (iv) ion-exchange to remove the M ions completely from the material and (v) calcination to obtain the zeolite in hydrogen form.
- MOH tetraethylammonium hydroxide
- this standard method gives a H-SUZ-4 catalyst with high density of acid sites, and it deactivates very rapidly during oxygenate (methanol) conversion to olefins.
- oxygenate methanol
- the drawback is the rapid deactiva- tion.
- the Si/Al ratio is then adjusted to the desired value by changing the amount of Al-wire dissolved in the aqueous MOH solution (i) .
- the Si/Al ratio can also be ad- justed to the desired value another way, i.e. by contacting the product with water vapour at elevated temperatures (so- called "steaming" .
- the steaming is preferably performed for a period of 1-12 hours by feeding 1-20 g 3 ⁇ 40 per g of catalyst per hour at a temperature of 400-700°C. After the steaming the resulting SUZ-4 catalyst is washed with an aqueous acid solution.
- the present invention is related to the use of the above- mentioned SUZ-4 zeolite material in the conversion of oxy- genates, especially methanol/dimethyl ether (DME) , to olefins.
- SUZ-4 zeolite material in the conversion of oxy- genates, especially methanol/dimethyl ether (DME)
- DME methanol/dimethyl ether
- SZR topology consisting of a 3-dimensional channel system of straight 10-rings and zig-zag 8-rings, a surprisingly high selectivity (60-70%) to light olefins (ethylene and propylene) is observed.
- a by-product approximately 10-20%) , olefins with a hydrocar ⁇ bon chain length in the gasoline range are obtained.
- the selectivity to aromatic hydrocarbons is typically below 2%.
- the calcined material as prepared was sub ⁇ jected to ion-exchange three times with an aqueous IN NH 4 NO 3 solution under reflux, washed with deionized wa ⁇ ter, dried at 120°C for 3 hours and then calcined at 550°C for 12 hours.
- the synthesis conditions used are
- H.S. means horizontal stirring
- SUZ-4a means SUZ-4 + amorphous .
- X-ray diffraction (XRD) data were analyzed using EVA 8.0, developed by SOCABIM. The diffraction pattern was compared with the data in the powder diffraction file (PDF) database compiled and revised by Joint Committee on Powder Diffraction Standards International Centre. Surface area
- the BET surface area of the SUZ-4 catalysts was deter ⁇ mined by nitrogen adsorption at a temperature of 77 K using a BELSORP-mini II instrument. Prior to the measurement the catalyst was pretreated for 5 hours (out- gassing for 1 hour at 80°C and for 4 hours at 300°C) .
- the calcined SUZ-4 catalysts were tested for the MTH reaction using a fixed bed reactor. 50 mg of catalysts and temperatures between 350 and 450 °C were used. The catalysts were pressed, gently crushed and sieved to a particle size of 0.25-0.42 mm. Before each test, the catalysts were calcined in situ at 550°C (see above) under a flow of oxygen for 1 hour. Helium was used as a carrier gas and methanol was fed using a bubble satura- tor placed in a water bath at 20°C. A methanol feed rate (expressed as WHSV, i.e. weight hourly space ve ⁇ locity, which is defined as the weight of feed flowing per unit weight of the catalyst per hour) of 2.05 gg _1 h _1 was used. The reaction products were analyzed by GC and GC-MS .
- the GC analyses were performed using an on-line gas chromatograph (Agilent 6890 A with FID) using a Supelco SPB-5 capillary column (60m, 0.530 mm i.d., stationary phase thickness 3ym) . The temperature was programmed between 45 and 260°C with a heating rate of 25 °C min -1 (hold time 5 min at 45°C and 16 min at the final tem ⁇ perature) .
- GC-MS analyses were performed using a HP 6890 gas chromatograph equipped with a GS-GASPRO column (60m, 0.32 mm) and a HP-5973 Mass Selective Detector. Each analysis took 40 minutes, and the temperature was programmed between 100 and 250 °C with a heating rate of 10°C min -1 (hold time 10 min at 100°C and 15 min at 250°C) . (c) Results
- Fig. 3 displays (a) TEM overview micrograph, (b) Micrograph and diffraction image (insert) of random crystallite.
- Fig. 5 displays GC-MS chromatograms of the methanol to hydrocarbon reaction over different zeolites, reaction carried out under identical conditions.
Abstract
A catalyst for the conversion of oxygenates, such as alcohols or ethers, to olefins consists essentially of a selected SUZ-4 zeolite that has a Si/A1 ratio of at least 20, preferably between 20 and 500, especially between 20 and 100. The basic SUZ-4 zeolite is prepared in a manner known per se, whereafter the Si/A1 ratio is increased to the desired value. The selected SUZ-4 zeolite catalyst of the invention has a longer life time and a better product selectivity than the conventional/standard SUZ-4 zeolite catalysts.
Description
Catalyst for the conversion of oxygenates to olefins and a process for preparing said catalyst
Technical Field
The present invention relates to a catalyst, which is suit¬ able for use in the process where oxygenates, i.e. chemical compounds containing oxygen as part of their structure (e.g. alcohols or ethers) are converted to olefins. A meth- od for the formation of the catalyst is also provided.
More specifically the invention concerns a catalyst for the conversion of oxygenates to olefins, said catalyst being based on SUZ-4 zeolite. The SUZ-4 zeolite is modified in a number of ways with the purpose to yield a catalyst with improved properties for the conversion of oxygenates to olefins .
Background to the Invention
SUZ-4 zeolite has been given the three-letter IUPAC designation code SZR. The framework of the SUZ-4 zeolite consists of 4-, 5-, 6-, 8- and 10-membered rings of 3- dimensional channel systems. It has an ortho-rhombic unit cell with dimensions of a = 18.8696, b = 14.4008 and c = 7.5140 A, respectively. The 10-membered ring channels of the SUZ-4 zeolite are the main straight channels in the framework, and they are interconnected by zig-zag 8-ring channels. The 10-ring straight channels of the SUZ-4 zeo- lite have dimensions of 4.6 x 5.2 A, i.e. notably smaller than the 10-ring channels found in the ZSM-5 zeolite (5.3 x 5.5 and 5.4 x 5.6 A) .
Within the catalyst area, the SUZ-4 zeolite is known to be a selective and stable dehydration catalyst in the process for producing dimethyl ether from methanol (Jiang, S. et al., Chemistry Letters 33, no. 8, 1048 (2004)).
According to US 6,936,562 B2 (General Motors Corp.), certain metal-exchanged SUZ-4 zeolites have been prepared which have catalytic activity in the reduction of NOx in the exhaust gas from a hydrocarbon or alcohol fuelled en¬ gine .
Similar hydrothermally-stable catalysts based on substi¬ tuted SUZ-4 zeolites are described in the related US
6,645,448 B2 (General Motors Corp.), and in US 5,118,483 B2 (British Petroleum Co.) various crystalline forms of the SUZ-4 zeolite based on crystalline (metallo) silicates are described. It should be noted that - with reference to e.g. US 5,118,483 - the standard methods for forming SUZ-4 zeo- lites will usually provide thermochemically-preferred Si/Al stoichiometries , regardless of the molar ratios of the Si and Al components in the starting materials.
EP 0 706 984 Al (BP Chemicals Ltd.) discloses the catalytic use of SUZ-4 zeolite for the isomerisation of hydrocarbons, and in US 6,514,470 B2 (University of California) a large number of aluminium-silicate materials, including SUZ-4 ze¬ olite, are used as catalysts for lean burn exhaust abate¬ ment. JP 2009-233620 A (Tosoh Corp.) describes the use of SUZ-4 zeolite in an SCR catalyst with the objective to give the catalyst improved hydrothermal durability.
Most recently, variants of the methanol to olefins (MTO) process have been disclosed in EP 1 963 241 A2 and in WO 2008/042616 A2 (both to UOP LLC) . One of the main challenges within the field of MTO cataly¬ sis is that the known catalysts have a very limited life span, requiring continuous regeneration at elevated temperature which eventually lead to irreversible damage to the catalyst. According to the inventors, this is also the case with the SUZ-4 zeolite-based catalysts, because the life span of the current SUZ-4 zeolite-based catalyst pre¬ pared using the standard methods in the MTO catalysis field does not exceed that of other catalysts such as silicoalu- minophosphate molecular sieves (e.g. SAPO-34). However, it has now surprisingly been found that the life span of the SUZ-4 zeolite-based catalyst for MTO use can be markedly improved by either modification of the zeolite acidity (i.e. by increasing the Si/Al ratio, partial ion-exchange of alkali counter-ions)
Summary of the Invention
The invention concerns a catalyst for the conversion of oxygenates to olefins, said catalyst consisting essentially of a selected SUZ-4 zeolite. The catalyst according to the invention is characterised in that the zeolite has a Si/Al ratio of at least 20, preferably between 20 and 500. The most preferred Si/Al ratio in the zeolite is between 20 and 100.
Furthermore, the invention concerns a process for the preparation of the catalyst, said method comprising the steps of:
(a) providing a conventional/standard SUZ-4 zeolite having a Si/Al ratio of less than 20, and
(b) increasing the Si/Al ratio to 20 or above by con- tacting the product of step (a) with water vapour at elevated temperatures.
In the above process, step (b) is preferably performed at a temperature of 400-700°C. Furthermore it is preferred to perform step (b) for 1-12 hours by feeding 1-20 g ¾0 per g of catalyst per hour.
The SUZ-4 catalyst resulting from step (b) of the process is preferably washed with an aqueous acid solution.
The catalyst according to the invention is used for the conversion of oxygenates to olefins. The oxygenates to be converted to olefins are preferably selected from the group consisting of CI to C4 alcohols. The most preferred oxygen- ate to be converted to an olefin is methanol.
Brief Description of the Figures
Figure 1 shows the XRD diffraction profile of SUZ-4 having gel Si/Al = 8 and 13.
Figure 2 shows an SEM image of SUZ-4 having Si/Al = 8 in the synthesis gel. Figure 3 shows a TEM image of an SUZ-4 zeolite-based cata¬ lyst having Si/Al = 8 in the synthesis gel.
Figure 4 shows the BET isotherm of SUZ-4 having gel Si/Al = 8 in the synthesis gel.
Fig. 5 shows GC-MS chromatograms of SAPO-34, SUZ-4, and ZSM-5 catalysts tested under identical reaction conditions after 5 minutes on stream. NB : CI is not included in the chromatogram. (400 °C and WHSV = 2.05 gg_1h_1)
Detailed description of the invention
According to the invention the selected SUZ-4 zeolite has a Si/Al ratio of at least 20, preferably between 20 and 500 as determined using SEM-EDX, ICP and ammonia TPD. A more preferred Si/Al ratio is between 20 and 100.
The SUZ-4 zeolite-based catalyst is synthesized in a manner known per se by preparing (i) a solution of Al-wire in aqueous MOH, where M is an alkali metal, (ii) a 25 wt% so¬ lution of tetraethylammonium hydroxide (TEAOH) and (iii) a 40 wt% solution of Ludox-AS 40, mixing the solutions (i)- (iii) at 60°C and crystallizing the resultant gel at 160°C with stirring, followed by (iv) ion-exchange to remove the M ions completely from the material and (v) calcination to obtain the zeolite in hydrogen form. According to the in- vention, this standard method gives a H-SUZ-4 catalyst with high density of acid sites, and it deactivates very rapidly during oxygenate (methanol) conversion to olefins. It should be noted that the conversion of methanol to olefins is novel in this work, the drawback is the rapid deactiva- tion. Thus, the Si/Al ratio is then adjusted to the desired value by changing the amount of Al-wire dissolved in the aqueous MOH solution (i) . The Si/Al ratio can also be ad-
justed to the desired value another way, i.e. by contacting the product with water vapour at elevated temperatures (so- called "steaming") . The steaming is preferably performed for a period of 1-12 hours by feeding 1-20 g ¾0 per g of catalyst per hour at a temperature of 400-700°C. After the steaming the resulting SUZ-4 catalyst is washed with an aqueous acid solution.
While it is known from the above citations that SUZ-4 zeo- lites may be used as catalysts in various contexts, the specific use of SUZ-4 zeolite materials as catalysts in the conversion of oxygenates to olefins is novel. Thus, the present invention is related to the use of the above- mentioned SUZ-4 zeolite material in the conversion of oxy- genates, especially methanol/dimethyl ether (DME) , to olefins. Due to the unique topology (SZR topology), consisting of a 3-dimensional channel system of straight 10-rings and zig-zag 8-rings, a surprisingly high selectivity (60-70%) to light olefins (ethylene and propylene) is observed. As a by-product (approximately 10-20%) , olefins with a hydrocar¬ bon chain length in the gasoline range are obtained. The selectivity to aromatic hydrocarbons is typically below 2%.
As a consequence of the selectivities observed, the
catalyst has a high potential to be used cL S cL C3.talyst for the production of light olefins (ethylene and pro¬ pylene) with a gasoline fraction having a low content of aromatic compounds as a co-product. Methane, which is also regarded as co-product during olefin produc- tion, could be used as a source for the necessary ex¬ ternal thermal energy for the MTO process.
The present invention will now be illustrated further in the following examples.
Example 1
(A) Synthesis of SUZ-4 zeolite using the standard method
An SUZ-4 zeolite was synthesized according to the procedure published by S. Jiang et al . , Chemistry Letters 33, no. 8, 1048 (2004) .
The following solutions were prepared:
(a) 0.4 g Al-wire dissolved in a KOH solution (3.3 g KOH in 50.6 g H20)
(b) 7.93 g TEAOH (25 wt%)
(c) 18.23 g LUDOX AS-40 (40 wt%).
To the clear solution (a) , solution (b) and solution (c) were added successively while stirring at 60°C. The batch composition of the synthesis mixture was
7.92 K20 : A1203 : 16.21 Si02 : 1.83 TEAOH : 507 H20. The gel was transferred to 40 ml Teflon lined stainless steel autoclaves. The Si/Al ratio was varied by chang¬ ing the amount of Al-wire dissolved in KOH solution. Crystallization of the gel was carried out under horizontal stirring conditions using a Teflon coated bar magnet at 160°C for 2 to 5 days. When the crystalliza¬ tion was complete, the reaction mixture was washed with distilled water, and the product was recovered by fil-
tration. The calcined material as prepared was sub¬ jected to ion-exchange three times with an aqueous IN NH4NO3 solution under reflux, washed with deionized wa¬ ter, dried at 120°C for 3 hours and then calcined at 550°C for 12 hours. The synthesis conditions used are
Table 1: Synthesis conditions used in the crystalliza- tion of SUZ-4 zeolite
*) In the above table, H.S. means horizontal stirring, and SUZ-4a means SUZ-4 + amorphous .
(B) Characterization and catalyst tests X-ray diffraction
The purity and crystallinity of the products were iden¬ tified using X-ray diffraction on a Siemens D-5000 diffractometer with Bragg-Brentano geometry, position sensitive detector and CuK l radiation (λ= 1.5406 A) . X-ray diffraction (XRD) data were analyzed using EVA 8.0, developed by SOCABIM. The diffraction pattern was compared with the data in the powder diffraction file (PDF) database compiled and revised by Joint Committee on Powder Diffraction Standards International Centre.
Surface area
The BET surface area of the SUZ-4 catalysts was deter¬ mined by nitrogen adsorption at a temperature of 77 K using a BELSORP-mini II instrument. Prior to the measurement the catalyst was pretreated for 5 hours (out- gassing for 1 hour at 80°C and for 4 hours at 300°C) .
Scanning and transmission electron microscopy
SUZ-4 crystals were sprinkled on a carbon tape mounted on a copper grid. The crystal size and shape were in¬ vestigated using Scanning Electron Microscopy, Quanta 200 F (FEI) . Similarly TEM images were taken and elec- tron diffraction revealed unit cell parameters and ori¬ entation of the 8- and 10-ring channels within the crystal .
The template was removed by calcination under static air at 550°C for 6 hours. The calcined samples were ion-exchanged for 3 x 2 hours with 1M NH4NO3 in a 70 °C water bath. The ion-exchanged catalysts were calcined at 550°C for 2 hours in static air, for 1 hour ex situ in a flow of pure oxygen, and for 1 hour in situ in the fixed bed reactor in a flow of pure oxygen prior to each catalytic experiment to desorb ammonia.
The calcined SUZ-4 catalysts were tested for the MTH reaction using a fixed bed reactor. 50 mg of catalysts and temperatures between 350 and 450 °C were used. The catalysts were pressed, gently crushed and sieved to a particle size of 0.25-0.42 mm. Before each test, the
catalysts were calcined in situ at 550°C (see above) under a flow of oxygen for 1 hour. Helium was used as a carrier gas and methanol was fed using a bubble satura- tor placed in a water bath at 20°C. A methanol feed rate (expressed as WHSV, i.e. weight hourly space ve¬ locity, which is defined as the weight of feed flowing per unit weight of the catalyst per hour) of 2.05 gg_1h_1 was used. The reaction products were analyzed by GC and GC-MS .
The GC analyses were performed using an on-line gas chromatograph (Agilent 6890 A with FID) using a Supelco SPB-5 capillary column (60m, 0.530 mm i.d., stationary phase thickness 3ym) . The temperature was programmed between 45 and 260°C with a heating rate of 25 °C min-1 (hold time 5 min at 45°C and 16 min at the final tem¬ perature) . GC-MS analyses were performed using a HP 6890 gas chromatograph equipped with a GS-GASPRO column (60m, 0.32 mm) and a HP-5973 Mass Selective Detector. Each analysis took 40 minutes, and the temperature was programmed between 100 and 250 °C with a heating rate of 10°C min-1 (hold time 10 min at 100°C and 15 min at 250°C) . (c) Results
Fig. 1 displays the XRD profiles of SUZ-4 having Si/Al ratios of 8 and 13 in the synthesis gel. By comparing the observed diffraction profile with a theoretically calculated diffraction profile (Fig.l bottom), it was observed that the product was free from structural im¬ purities .
Fig. 2 and Fig. 3 respectively displays the SEM and TEM image of an SUZ-4 zeolite-based catalyst having Si/Al = 8 in the synthesis gel. The crystals were needle-shaped and -2-3 ym in length.
Fig. 3 displays (a) TEM overview micrograph, (b) Micrograph and diffraction image (insert) of random crystallite. Fig. 4 displays the BET isotherm for the SUZ-4 catalyst having Si/Al = 8. The isotherm is typical for a micro- porous material. The surface area of the catalyst was found to be 346 m2/g. Fig. 5 displays GC-MS chromatograms of the methanol to hydrocarbon reaction over different zeolites, reaction carried out under identical conditions.
Example 2
Determination of methanol conversion
Table 2 below shows the percentage methanol conversion and the product selectivities at different reaction temperatures; WHSV = 2.05 gg_1h_1 was used. At 350°C the initial conversion of the catalyst was 83%, and the catalyst showed a very high selectivity for CI (21%, second most abundant species) . Increasing the tempera¬ ture to 400 and 450°C improved the initial conversion by the catalyst to -100%, the selectivity for CI was decreased by approximately a factor of 2. At these re-
action temperatures, C2 and C3 were the most abundant species (C2 + C3 > 60%) .
Table 2 : Methanol conversion, product selectivity and C4 hydrogen transfer index of SUZ-4 catalyst for the MTH reaction at different reaction temperatures after 3 minutes on stream, Si/Al = 8. (WHSV = 2.05 gg_1h_1)
It is firmly believed that the high selectivity towards C2 and C3 is caused by the needle-like morphology of the catalyst crystals, as seen by SEM. A simulation of crystal growth indicates that the 10-ring channels run in the direction of the needles. If these needles are described as cylinders, the simulation result means that only the two bases of each cylinder serve as exits through 10-ring channels. The major part of the exter- nal crystal surface will serve as exits through 8- rings, which are orthogonal to the 10-rings. This gives rise to a product shape selectivity dominated by 8- rings, leading to high selectivities towards C2 and C3.
The SUZ-4 sample tested deactivates very fast. After 43 minutes (the effluent is sampled every 40 minutes) , the conversion was negligible. This is consistent with the relatively high selectivity towards CI (and also pro- pane) , which is inherently linked to formation of aro- matics and coke. This rapid deactivation may well be attributed to the very high Al content in the sample, which means that the density of acid sites is untypi- cally high for methanol conversion catalysts.
Example 3
Comparison of SUZ-4 to ZSM-5 and SAPO- For the sake of comparison, ZSM-5 and SAPO-34 were tested for the MTH reaction under identical reaction conditions as those of SUZ-4, and the results are pre¬ sented in Fig. 5 and Table 3. Note that SAPO-34 is cur¬ rently used as a commercial MTO catalyst. Table 3 dis- plays the product selectivities for the three different zeolites at 400°C. The GC analyses were performed after 3 minutes on stream, and the catalysts displayed ap¬ proximately 100% conversion. ZSM-5 catalyst has high selectivity for heavier hydrocarbons than SUZ-4 and SAPO-34 catalysts (see Fig. 5 and Table 3) .
Catalyst CI C2 C3 C4alkene
ZSM-5 0.28 7.58 21.20 8.77
SUZ-4 10.24 24.35 37.71 14.11
SAPO-34 0.56 29.65 42.59 16.70
Table 3: Product selectivity of the MTH reaction over ZSM-5, SAPO-34, and SUZ-4 catalysts, WHSV = 2, 400°C, and full conversion of methanol
The C4 alkane selectivity of the ZSM-5 catalyst is no¬ tably higher than both that of the inventive SUZ-4 cat- alyst and that of the SAPO-34 catalyst, giving rise to a higher C4 hydrogen transfer index. Except for the selectivity for methane (CI), the SAPO-34 and SUZ-4 cata¬ lysts showed comparable product selectivities for all the other hydrocarbons. For both materials C2 and C3 were the most abundant species (SAPO-34 C2+C3 = 72.3 and SUZ-4 C2+C3 = 61.1). The inventive SUZ-4 catalyst showed a much higher selectivity for methane (approxi¬ mately 10%) than SAPO-34 (>1%) .
Claims
Catalyst for the conversion of oxygenates to ole¬ fins, said catalyst consisting essentially of a se¬ lected SUZ-4 zeolite, characterised in that the zeo¬ lite has a Si/Al ratio of at least 20, preferably between 20 and 500.
Catalyst according to claim 1, characterised in that the zeolite has a Si/Al ratio of between 20 and 100.
A process for the preparation of a catalyst accord¬ ing to claim 1 or 2, said method comprising the steps of:
(a) providing a conventional/standard SUZ-4 zeolite having a Si/Al ratio of less than 20, and
(b) increasing the Si/Al ratio to above 20 by con¬ tacting the product of step (a) with water vapour at elevated temperatures.
Process according to claim 3, characterised in that step (b) is performed at a temperature of 400-700°C.
Process according to claim 3 or 4, characterised in that step (b) is performed for 1-12 hours by feeding 1-20 g ¾0 per g of catalyst per hour.
Process according to any one of claims 3-5, characterised in that the SUZ-4 catalyst resulting from step (b) is washed with an aqueous acid solution.
The use of the catalyst according to claim 1 or 2 in the conversion of oxygenates to olefins.
The use according to claim 7, wherein the oxygenates are selected from the group consisting of CI to C4 alcohols .
9. The use according to claim 8, wherein the oxygenate is methanol.
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